WO2006038325A1 - Appareil de traitement d’eau pour pile a combustible - Google Patents

Appareil de traitement d’eau pour pile a combustible Download PDF

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Publication number
WO2006038325A1
WO2006038325A1 PCT/JP2005/004935 JP2005004935W WO2006038325A1 WO 2006038325 A1 WO2006038325 A1 WO 2006038325A1 JP 2005004935 W JP2005004935 W JP 2005004935W WO 2006038325 A1 WO2006038325 A1 WO 2006038325A1
Authority
WO
WIPO (PCT)
Prior art keywords
fuel cell
water
water treatment
resin
adsorption
Prior art date
Application number
PCT/JP2005/004935
Other languages
English (en)
Japanese (ja)
Inventor
Masayuki Miwa
Yoshiteru Misumi
Original Assignee
Kurita Water Industries Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from JP2004286370A external-priority patent/JP5082188B2/ja
Application filed by Kurita Water Industries Ltd. filed Critical Kurita Water Industries Ltd.
Publication of WO2006038325A1 publication Critical patent/WO2006038325A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
    • H01M8/04156—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04291—Arrangements for managing water in solid electrolyte fuel cell systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/12—Halogens or halogen-containing compounds
    • C02F2101/14—Fluorine or fluorine-containing compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention relates to a water treatment device for a fuel cell that treats water recovered from a fuel cell with an electrodeionization device, and particularly to a water treatment for a fuel cell that is suitable when the fuel cell is a polymer electrolyte fuel cell. Relates to the device.
  • the fuel cell is a phosphoric acid fuel cell.
  • the fuel cell is a polymer electrolyte fuel cell.
  • a fluorine-based cation exchange membrane is used as a solid electrolyte, and the fuel cell wastewater contains a small amount of fluorine ions.
  • An object of the present invention is to provide a water treatment device for a fuel cell which is improved to sufficiently remove fluorine from water flowing into an electrodeionization device.
  • a water treatment apparatus for a fuel cell includes a fluorine adsorption unit that performs a fluorine adsorption treatment on the recovered water collected from the fuel cell, and an electrodeionization device that deionizes the water treated by the fluorine adsorption unit. And have.
  • fluorine is highly adsorbed and removed by the fluorine adsorption / removal device from the water from the fuel cell, so that the ion exchanger of the electrodeionization device is deteriorated by fluorine.
  • Water treatment can be performed.
  • FIG. 1 is a flow chart of a fuel cell water treatment device according to an embodiment.
  • FIG. 2 is a perspective view of the fuel cell water treatment device of FIG.
  • FIG. 3 is a perspective view of the casing of FIG. 2 with the front cover opened.
  • FIG. 3 is also a perspective view of the state where the fluorine adsorbent resin and the metal adsorbed resin are removed.
  • FIG. 5 is a front view showing the configuration of FIG. 4.
  • FIG. 6a and FIG. 6b are perspective views of the frame in the air cleaning chamber.
  • FIG. 7 is a cross-sectional view taken along line VII-VII in FIG.
  • FIG. 8 is a perspective view of a spiral plate in the decarbonation chamber.
  • FIG. 9 is a flow diagram of a fuel cell water treatment device according to another embodiment.
  • FIG. 10 is a flow diagram of a fuel cell water treatment device according to yet another embodiment. Detailed description of preferred embodiments and forms of the invention
  • a decarboxylation means may be provided before the fluorine adsorption removal means.
  • a decarboxylation means may be provided between the fluorine adsorption removal means and the electrodeionization apparatus.
  • the fuel cell recovered water may include water recovered from exhaust gas containing a large amount of carbon dioxide gas such as exhaust gas from a fuel reformer.
  • a water treatment device When such recovered water is treated with a water treatment device, it is decarboxylated by a decarboxylation means in advance before flowing into the electrodeionization device, thereby reducing the load on the electrodeionization device. The power consumption of the device can be reduced.
  • Metal adsorption removal means may be provided between the fluorine adsorption removal means and the electrodeionization apparatus.
  • Metal adsorption removing means may be provided between the decarboxylation means and the electrodeionization apparatus.
  • a metal adsorption / removal unit may be provided between the fluorine adsorption / removal unit and the decarboxylation unit.
  • the fluorine adsorption removal means force is temporarily reduced to metal ions such as cerium and aluminum. Metal ions that flow into the electrodeionization device even if Can be reduced. As a result, the performance of the ion exchanger of the electrodeionization apparatus can be maintained high over a long period of time.
  • the fluorine adsorption / removal means is preferably a fluorine adsorption resin, an anion exchange resin or an alumina compound (eg, acid aluminum).
  • the metal adsorption removing means is preferably a metal adsorption resin, a chelate resin or a cation exchange resin.
  • the TOC elution amount of these coagulates is 200 ppb or less.
  • the electrodeionization apparatus is contaminated by the resin, and the coagulant components are mixed in the treated water of the electrodeionization apparatus. It is prevented.
  • a gas-liquid contact type or membrane type decarboxylation apparatus is suitable. It is preferable to supply air to the gas phase side of the decarboxylation device using an air supply device to the fuel cell air electrode. Specifically, the outlet force air of this air supply device is collected and supplied to the gas phase side of the decarbonation means. In the case of claim 13, part or all of the fuel cell air electrode exhaust may be supplied to the gas phase side of the decarbonation means.
  • FIG. 1 is a flow diagram of a fuel cell water treatment apparatus according to an embodiment of the present invention.
  • the recovered water such as condensate from the fuel cell is treated by the decarboxylation device 1, the fluorine adsorption removal device 2, the metal removal device 3 and the electrical deionization device 4, and the deionized water produced by the electrical deionization device 4 is used as fuel. Supplied to a reformer or the like.
  • a cation exchange membrane and a ion exchange membrane are arranged between an anode and a cathode to form a desalting chamber and a concentration chamber, and an ion exchanger is placed in the desalting chamber. It may be of a filled configuration.
  • the anode chamber and the cathode chamber may be provided independently, or at least one of these electrode chambers may also serve as the concentration chamber.
  • the decarboxylation device 1 is of the air aeration type.
  • the aeration air is published in the air cleaning device 5 and purified, and then blown into the water in the decarbonation device 1.
  • the air cleaning device 5 is connected to the concentration chamber or electrode chamber force of the electrodeionization device 4. Drainage is introduced. The waste water from the air cleaning device 5 is discharged out of the system.
  • fluorine is highly adsorbed and removed from the fuel cell recovered water by the fluorine adsorption / removal device 2, and therefore the ion exchanger of the electrodeionization device 4 Is prevented from being deteriorated by fluorine, and the fuel cell wastewater can be treated stably over a long period of time and used as a water source for the fuel reformer.
  • the decarbonation device, the fluorine adsorption removal device, and the metal removal device are provided with a pretreatment device arranged in a casing, and an electrodeionization device 4 attached to the pretreatment device.
  • the fuel cell water treatment apparatus will be described with reference to FIGS.
  • FIG. 2 is a perspective view of the fuel cell water treatment device as viewed from below
  • Fig. 3 is a perspective view of the casing with the front cover opened
  • Fig. 4 is a fluorine diagram from Fig. 3.
  • FIG. 5 is a front view showing the configuration of FIG. 4
  • FIG. 6 is a perspective view of the frame in the air-cleaning chamber
  • FIG. 7 is FIG.
  • FIG. 8 is a perspective view of the spiral plate in the decarbonation chamber.
  • this water treatment apparatus for a fuel cell is one in which the pretreatment device 10 and the electrodeionization device 4 are integrated.
  • the casing 12 of the pretreatment device 10 has a shallow rectangular parallelepiped shape, and a front cover 14 is attached to the front.
  • waste water from the concentration chamber or electrode chamber of the electrodeionization apparatus 4 is introduced into the air cleaning chamber 20 through the transfer pipe 18 and air is cleaned.
  • the configuration of the air cleaning chamber 20 will be described in detail later.
  • the air cleaned in the air cleaning chamber 20 is introduced from the air inlet 31 into the decarbonation chamber 30, and the water used for cleaning flows out from an outflow hole (not shown) provided on the back surface of the casing 12. And discarded.
  • To-be-treated water is introduced into the upper part of the decarbonation chamber 30 from the treated water inlet (not shown) on the back surface or upper surface of the casing 12.
  • the air from the air inlet 31 rises while circling the spiral plate 32, contacts with the water to be treated, and decarboxylates.
  • the spiral passage 34 of the spiral plate 32 is filled with a packing (not shown) having a random structure in which a wire is entangled. It is configured to be fully decarboxylated.
  • the diameter of the wire is preferably about 0.05 to 0.5 mm.
  • the average diameter of the path between the wires of the filler is preferably 2-10 mm, especially 3-7 mm.
  • the spiral plate 32 is obtained by joining a metal plate with a slit and bending it in multiple stages by welding or the like, and a long and narrow partition plate is vertically passed through the spiral shaft center.
  • the height of one spiral is about 5-10mm.
  • the metal plate constituting each step of the spiral plate 32 has a rectangular shape.
  • the spiral plate has a screw shape.
  • the decarbonation chamber 30 has a height of 100 mm, a depth and a width of 50 mm. As shown in the figure, a seven-stage spiral plate 32 is arranged, and a packing having an average opening diameter of about 5 mm is filled into the spiral flow path.
  • a water temperature of 5 ° C and a carbonate concentration of 80 ppm was passed through the decarboxylation device at 40 mLZmin and the air was diffused at 200 OmLZmin, the carbonate concentration of the treated water was found to be lOppm or less. It was.
  • the decarboxylated water flows into the relay chamber 40 (Figs. 4 and 7) from the decarboxylation chamber 30 via the advection port 36 (Fig. 5) and from the relay chamber 40 to the advection port. 42 (Fig. 7) into the reservoir 50.
  • the relay chamber 40 is extended in the vertical direction behind the water storage chamber 50.
  • a water advection port 42 force S is provided at the upper part of the relay chamber 40.
  • float switches 52 and 54 for detecting the water level are provided in the water storage chamber 50. When both the float switches 52 and 54 are OFF, the pump 62 described below is stopped.
  • the water in the water storage chamber 50 is introduced into the lower portion of the first fluorine removal chamber 70 through the tube 60, the pump 62 driven by the motor 64, and the tube 66, and rises in the chamber 70. .
  • water is introduced into the upper part of the second fluorine removing chamber 72 from the upper part of the fluorine removing chamber 70 via the advection pipe 71 and descends in the chamber 72.
  • it is introduced into the lower part of the third fluorine removal chamber 74 through the advection port 73 and moves up in the chamber 74.
  • Each fluorine removal chamber 70, 72, 74 is filled with fluorine adsorption resin 76 (Fig. 3), and fluorine ions are adsorbed and removed.
  • fluorine adsorption resin 76 an alumina compound having fluorine adsorption ability such as alumina silicate can also be used.
  • the water that has reached the upper part of the third fluorine removing chamber 74 is transferred from the advancing port 78 to the upper part of the first metal removing chamber 80, and descends in the chamber 80. Next, it flows into the lower part of the second metal removal chamber 82 from the advection port 81 and ascends in the chamber 82. The water reaching the upper part of the chamber 82 is introduced into the electrodeionization apparatus 4 through the advection port 84.
  • a microfiltration membrane is disposed so as to cover the advection port 84 so that the debris does not flow into the electrodeionization device 4.
  • Each of the metal removal chambers 80 and 82 is filled with a metal adsorption resin 86, and metal ions are adsorbed and removed.
  • the water decarboxylated, fluorine-removed and metal-removed by the pretreatment device 10 is introduced into the electrodeionization device 4 through the advection port 84.
  • partition plates 90, 92, 94, 96, 98 force S are vertically extended in order to partition each removal chamber 70, 72, 74, 80, 82, Each chamber 70, 72, 74, 80, 82 extends in the vertical direction.
  • the tube 66 passes through the partition plate 90, and the advection pipe 71 passes through the partition plate 92.
  • the advection ports 73, 78, 81 are provided in the partition plates 94, 96, 98.
  • the advection port 84 is formed in the side wall of the casing 12.
  • FIGS. 6a and 6b are perspective views showing forces in opposite directions.
  • FIG. 6b the water staying in the cleaning chamber 20 is shown.
  • the air cleaning chamber 20 is formed between a pair of vertical partition plates 20a and 20b (FIG. 5) provided integrally with the casing 12.
  • Air sent from an air pump (not shown) is blown into the air cleaning chamber 20 through an air tube 21.
  • a frame 22 is installed in the air cleaning chamber 20.
  • the frame 22 includes a surrounding frame portion 23, a hanging plate 24, and a rising plate 25, and a central chamber 26, a water outflow chamber 27, and an air outflow chamber 28 are formed.
  • the end of the tube 21 is inserted into the central chamber 26.
  • Water is introduced into the central chamber 26 via the transfer pipe 18.
  • a drooping plate 24 that hangs down from the upper side of the surrounding frame portion 23 is provided between the outflow chamber 27 and the water in the central chamber 26 flows around the lower end of the drooping plate 24 to the water outflow chamber 27.
  • the central chamber 26 and the air outflow chamber 28 are partitioned by a rising plate 25 that stands up from the bottom side of the surrounding frame portion 23.
  • the air blown into the water from the tube 21 detaches from the water surface, then wraps around the upper end of the rising plate 25 and flows into the air outflow chamber 28, and the decarbonation chamber through the air introduction port 31. It is blown into 30 and used for decarboxylation as described above.
  • FIGS. 9 and 10 are flow charts of a fuel cell water treatment apparatus according to another embodiment of the present invention.
  • the fluorine adsorption / removal device 2 is placed in front of the decarboxylation device 1 and processed in the order of fluorine adsorption removal ⁇ decarbonation ⁇ metal removal ⁇ electrodeionization! /
  • Other configurations are the same as those in FIG.
  • Fig. 10 in Fig. 9, the decarboxylation device 1 is arranged on the rear stage side of the metal removal device 3, and the treatment is performed in the order of fluorine adsorption removal-> metal removal-> decarboxylation-> electrodeionization.
  • the rest of the configuration is the same as in Figure 9.
  • the fluorine is highly adsorbed and removed by the fluorine adsorption / removal device 2 from the fuel cell collected water.
  • the ion exchanger of device 4 is prevented from being deteriorated by fluorine, and the fuel cell waste water can be treated stably over a long period of time and used as a water source for the fuel reformer.
  • the fluorine adsorption resin used in the fluorine adsorption removal means, the anion exchange resin, the metal adsorption resin, chelate resin, and cation exchange resin used in the metal adsorption removal means There are molecules with unstable bonds and unpolymerized molecules. When the temperature rises, the molecules with unstable bonds and unpolymerized molecules are eluted from the resin into water.
  • the temperature of the fuel cell recovered water rises to about 65 ° C, it is placed in front of the electrodeionization device! As a result, the amount of effluent from the fluorine adsorption removal means and metal adsorption removal means increases, resulting In addition to contaminating the ion exchanger of the deionizer and lowering the performance, it also flows out into the treated water, reducing the purity of the treated water.
  • the main effluent of the filler material is TOC. Therefore, it is possible to use the TOC elution amount as an indicator of the cleanliness of the filler. By using a filler with a TOC elution amount of 200 ppb or less, contamination of the electrodeionization equipment, TOC component in the treated water Can be prevented.
  • the TOC elution amount is the value obtained by (Inlet TOC concentration) (Outlet TOC concentration)
  • the metal removing device 3 may be omitted in the flows of FIGS.
  • the decarbonation means may be a gas-liquid contact type other than the aeration type as described above.
  • the decarboxylation means may be a membrane type.
  • an air supply device provided in the fuel cell power generation device to the fuel cell air electrode may be used. In this way, it is possible to reduce the size of the apparatus without the need to provide an air supply source such as a blower, a fan, or a compressor inside the water treatment apparatus.
  • an air supply source such as a blower, a fan, or a compressor inside the water treatment apparatus.
  • exhaust containing generated water generated by reaction inside the fuel cell can be used. In this case, the generated water in the exhaust gas to be used can be taken in by gas-liquid contact, so that the recovered water utilization rate of the fuel cell power generation device can be improved.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Electrochemistry (AREA)
  • Water Supply & Treatment (AREA)
  • General Chemical & Material Sciences (AREA)
  • Sustainable Energy (AREA)
  • Sustainable Development (AREA)
  • Health & Medical Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Analytical Chemistry (AREA)
  • Molecular Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Urology & Nephrology (AREA)
  • Physical Water Treatments (AREA)
  • Fuel Cell (AREA)

Abstract

L’invention concerne un appareil de traitement d’eau pour pile à combustible, dans lequel l’eau récupérée d’une pile à combustible est traitée au moyen d’une unité de désionisation électrique, qui est amélioré de manière à assurer une défluoration satisfaisante de l’eau s’écoulant dans l’unité de désionisation électrique. L’eau résiduaire provenant d’une chambre d’électrode négative d’une unité de désionisation électrique (4) est introduite, par un tuyau de transfert (18), dans une chambre de lavage à l’air (20) dans laquelle un lavage à l’air est effectué. L’eau obtenue est décarboxylée dans une chambre de décarboxylation (30), et est amenée, au moyen d’une pompe (62), à s’écouler successivement à travers des chambres de défluorination (70,72,74) et des chambres de démétalllisation (80,82) avant d’être introduite dans l’unité de désionisation électrique (4).
PCT/JP2005/004935 2004-09-30 2005-03-18 Appareil de traitement d’eau pour pile a combustible WO2006038325A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2004-286370 2004-09-30
JP2004286370A JP5082188B2 (ja) 2003-10-01 2004-09-30 燃料電池用水処理装置

Publications (1)

Publication Number Publication Date
WO2006038325A1 true WO2006038325A1 (fr) 2006-04-13

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Application Number Title Priority Date Filing Date
PCT/JP2005/004935 WO2006038325A1 (fr) 2004-09-30 2005-03-18 Appareil de traitement d’eau pour pile a combustible

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WO (1) WO2006038325A1 (fr)

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000093976A (ja) * 1998-09-25 2000-04-04 Mitsubishi Chemicals Corp 純水の製造方法及び純水製造装置
JP2000279967A (ja) * 1999-03-29 2000-10-10 Japan Organo Co Ltd 脱イオン水製造装置
JP2000331703A (ja) * 1999-05-24 2000-11-30 Japan Organo Co Ltd 燃料電池における水回収装置
JP2001047054A (ja) * 1999-08-11 2001-02-20 Kurita Water Ind Ltd 脱イオン水製造装置の殺菌方法及び脱イオン水の製造方法
JP2001170658A (ja) * 1999-12-17 2001-06-26 Kurita Water Ind Ltd フッ素含有排水の処理装置及び処理方法
JP2001219161A (ja) * 2000-02-08 2001-08-14 Nomura Micro Sci Co Ltd 純水製造装置
JP2001259376A (ja) * 2000-03-16 2001-09-25 Japan Organo Co Ltd 脱イオン水製造装置
JP2002313404A (ja) * 2001-04-13 2002-10-25 Mitsubishi Heavy Ind Ltd 固体高分子型燃料電池システム
JP2002343388A (ja) * 2001-05-21 2002-11-29 Mitsubishi Chemicals Corp 燃料電池へ供給する水の処理方法
JP2004022200A (ja) * 2002-06-12 2004-01-22 Aisan Ind Co Ltd フッ素吸収装置及び該装置を備えた燃料電池システム
JP2004216302A (ja) * 2003-01-16 2004-08-05 Kurita Water Ind Ltd 電気脱イオン装置及び水処理装置
JP2005103492A (ja) * 2003-10-01 2005-04-21 Kurita Water Ind Ltd 脱炭酸装置
JP2005116184A (ja) * 2003-10-02 2005-04-28 Kurita Water Ind Ltd 燃料電池用水処理装置

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000093976A (ja) * 1998-09-25 2000-04-04 Mitsubishi Chemicals Corp 純水の製造方法及び純水製造装置
JP2000279967A (ja) * 1999-03-29 2000-10-10 Japan Organo Co Ltd 脱イオン水製造装置
JP2000331703A (ja) * 1999-05-24 2000-11-30 Japan Organo Co Ltd 燃料電池における水回収装置
JP2001047054A (ja) * 1999-08-11 2001-02-20 Kurita Water Ind Ltd 脱イオン水製造装置の殺菌方法及び脱イオン水の製造方法
JP2001170658A (ja) * 1999-12-17 2001-06-26 Kurita Water Ind Ltd フッ素含有排水の処理装置及び処理方法
JP2001219161A (ja) * 2000-02-08 2001-08-14 Nomura Micro Sci Co Ltd 純水製造装置
JP2001259376A (ja) * 2000-03-16 2001-09-25 Japan Organo Co Ltd 脱イオン水製造装置
JP2002313404A (ja) * 2001-04-13 2002-10-25 Mitsubishi Heavy Ind Ltd 固体高分子型燃料電池システム
JP2002343388A (ja) * 2001-05-21 2002-11-29 Mitsubishi Chemicals Corp 燃料電池へ供給する水の処理方法
JP2004022200A (ja) * 2002-06-12 2004-01-22 Aisan Ind Co Ltd フッ素吸収装置及び該装置を備えた燃料電池システム
JP2004216302A (ja) * 2003-01-16 2004-08-05 Kurita Water Ind Ltd 電気脱イオン装置及び水処理装置
JP2005103492A (ja) * 2003-10-01 2005-04-21 Kurita Water Ind Ltd 脱炭酸装置
JP2005116184A (ja) * 2003-10-02 2005-04-28 Kurita Water Ind Ltd 燃料電池用水処理装置

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